CN104383704B - A kind of step heating system to the preheating of gas fractionator inlet feed - Google Patents
A kind of step heating system to the preheating of gas fractionator inlet feed Download PDFInfo
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- 238000010438 heat treatment Methods 0.000 title claims abstract description 44
- 239000000463 material Substances 0.000 claims abstract description 125
- 238000005194 fractionation Methods 0.000 claims abstract description 69
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 50
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims abstract description 46
- 238000000034 method Methods 0.000 claims abstract description 43
- 239000002918 waste heat Substances 0.000 claims abstract description 31
- 238000010521 absorption reaction Methods 0.000 claims abstract description 23
- 239000007789 gas Substances 0.000 claims abstract description 18
- 239000000498 cooling water Substances 0.000 claims description 16
- 238000005504 petroleum refining Methods 0.000 claims description 10
- 239000006096 absorbing agent Substances 0.000 claims description 4
- 238000011084 recovery Methods 0.000 abstract description 5
- 238000001816 cooling Methods 0.000 abstract description 3
- 239000003208 petroleum Substances 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 description 7
- -1 alcohol amine Chemical class 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
本发明涉及一种对气体分馏塔进口物料预热的梯级加热系统，包括石油分馏加热系统组件及回收余热加热进口物料系统组件，其中：气体分馏加热系统组件包括：分馏塔、空冷器、水冷换热器及重沸器；回收余热加热进口物料系统组件包括：热水/物料换热器及蒸汽型溴化锂吸收式热泵；由热水/物料换热器在分馏塔外对物料预热升温至80±10℃，预热后的物料进入分馏塔，在塔内被塔底重沸器加热并维持在物料分馏所需的工作温度，实现物料的梯级加热。其优点是：利用回收的余热对进口物料进行预热，实现了分馏塔加热工艺的能量梯级利用，降低工艺蒸汽消耗量20％以上，提高了能源利用率，节约了成本。
The invention relates to a cascaded heating system for preheating the inlet materials of a gas fractionation tower, including petroleum fractionation heating system components and waste heat recovery heating inlet material system components, wherein: the gas fractionation heating system components include: fractionation towers, air coolers, water cooling Heater and reboiler; waste heat is recovered to heat the imported material system components include: hot water/material heat exchanger and steam type lithium bromide absorption heat pump; the hot water/material heat exchanger preheats the material to 80°C outside the fractionation tower ±10°C, the preheated material enters the fractionation tower, is heated by the reboiler at the bottom of the tower and maintained at the working temperature required for material fractionation, and realizes the cascade heating of the material. Its advantages are: the recovered waste heat is used to preheat the imported materials, the energy cascade utilization of the heating process of the fractionation tower is realized, the steam consumption of the process is reduced by more than 20%, the energy utilization rate is improved, and the cost is saved.
Description
技术领域technical field
本发明属于石油炼化生产领域，涉及一种对气体分馏塔进口物料预热的梯级加热系统，特别涉及到回收气体分馏塔塔顶产品物料余热及石油炼化其他工艺热联合余热对分馏塔进口物料梯级加热的系统。The invention belongs to the field of petroleum refining and chemical production, and relates to a cascaded heating system for preheating materials at the inlet of a gas fractionation tower, in particular to recovery of waste heat from materials at the top of the gas fractionation tower and combined waste heat from other processes of petroleum refining to the inlet of the fractionation tower Material cascade heating system.
背景技术Background technique
随着国民经济的迅速发展，社会对石油化工产品的需求日益增长，该行业能源消耗量占全国能源消耗总量的10％以上。而石油炼化厂生产中，气体分馏工艺环节是用热大户，常规气体分馏工艺系统流程如图1所示，主要包含以下几个主要部分：分馏塔1、重沸器2、空冷器3、水冷换热器4以及用于连接上述设备的管路、阀门等。常温物料由物料入口P1直接进入分馏塔，由塔底重沸器加热并维持至工作温度，塔顶出口的产品热物料依次经过空冷器和水冷换热器冷却后至物料出口P2。With the rapid development of the national economy, the social demand for petrochemical products is increasing, and the energy consumption of this industry accounts for more than 10% of the total energy consumption in the country. In the production of petroleum refineries, the process of gas fractionation is a large heat consumer. The process flow of the conventional gas fractionation process system is shown in Figure 1, which mainly includes the following main parts: fractionation tower 1, reboiler 2, air cooler 3, Water-cooled heat exchanger 4 and pipelines, valves, etc. for connecting the above-mentioned equipment. The material at room temperature enters the fractionation tower directly from the material inlet P1, and is heated by the reboiler at the bottom of the tower to maintain the working temperature. The product hot material at the top outlet of the tower is cooled by the air cooler and the water-cooled heat exchanger in turn to the material outlet P2.
其缺点1为：分馏塔塔顶出口的产品热物料(油气)的余热通过空冷器、水冷换热器及其循环水系统散失到环境中，造成大量的能量浪费。Its disadvantage 1 is: the waste heat of the product heat material (oil gas) at the top outlet of the fractionation tower is lost to the environment through the air cooler, water-cooled heat exchanger and its circulating water system, resulting in a large amount of energy waste.
其缺点2为：分馏塔的常温(20℃左右)进口物料经塔底重沸器加热并维持至工作温度，其中醇胺再生、脱丙烷、催化蒸馏等工艺的塔底物料工作温度约为110℃，重沸器通常以压力为0.3MPa左右的工艺蒸汽作为加热热媒，这种加热模式存在较大的换热温差，加热环节的熵增较大，能源的利用不合理。Disadvantage 2 is: the normal temperature (about 20°C) inlet material of the fractionation tower is heated by the bottom reboiler and maintained to the working temperature, and the working temperature of the bottom material of the alcohol amine regeneration, depropanization, catalytic distillation and other processes is about 110 ℃, the reboiler usually uses process steam with a pressure of about 0.3MPa as the heating medium. This heating mode has a large heat exchange temperature difference, the entropy increase in the heating link is large, and the use of energy is unreasonable.
发明内容Contents of the invention
本发明的目的是针对现有分馏塔物料加热工艺流程的不足，提出一种对气体分馏塔进口物料预热的梯级加热系统。特别提出一种利用蒸汽型溴化锂吸收式热泵回收分馏塔塔顶余热对进口物料预热的梯级加热系统，可以有效回收分馏塔塔顶出口产品热物料余热制备热水，通过热水/物料换热器对分馏塔进料进行预热；在有稳定的其它工艺环节热联合余热热媒水时，可代替蒸汽型溴化锂吸收式热泵作为热水/物料换热器的加热热源对分馏塔进口物料进行预热。本发明解决其技术问题所采用的方案如下：The object of the present invention is to propose a cascaded heating system for preheating the inlet materials of the gas fractionation tower, aiming at the deficiency of the material heating process of the existing fractionation tower. In particular, a cascaded heating system is proposed that utilizes the steam-type lithium bromide absorption heat pump to recover the waste heat at the top of the fractionation tower to preheat the imported materials, which can effectively recover the waste heat of the hot materials at the top of the fractionation tower to prepare hot water, and exchange heat through hot water/materials The device preheats the feed to the fractionation tower; when there is stable heat in other process links combined with waste heat heat medium water, it can replace the steam type lithium bromide absorption heat pump as the heating heat source of the hot water/material heat exchanger to heat the inlet material of the fractionation tower warm up. The scheme adopted by the present invention to solve its technical problems is as follows:
一种利用余热对气体分馏塔进口物料预热的梯级加热系统，包括气体分馏加热系统组件及回收余热加热进口物料系统组件，其中：所述的气体分馏加热系统组件包括：分馏塔、空冷器、水冷换热器及重沸器，分馏塔塔顶物料出口接空冷器物料侧入口，空冷器物料侧出口接水冷换热器物料侧入口；水冷换热器水侧接循环冷却水系统；重沸器的低温侧接分馏塔，重沸器高温侧接高温工艺蒸汽；所述的回收余热加热进口物料系统组件包括：热水/物料换热器及蒸汽型溴化锂吸收式热泵，其中：热水/物料换热器物料侧接分馏塔物料入口，热水/物料换热器热水侧接蒸汽型溴化锂吸收式热泵冷凝器及吸收器，蒸汽型溴化锂吸收式热泵发生器接高温工艺蒸汽，蒸汽型溴化锂吸收式热泵蒸发器接循环冷却水；由热水/物料换热器在分馏塔外对物料预热升温至80±10℃，预热后的物料进入分馏塔，在塔内被塔底重沸器加热并维持在物料分馏所需的工作温度，实现物料的梯级加热。A cascaded heating system that utilizes waste heat to preheat the inlet materials of a gas fractionation tower, including gas fractionation heating system components and recovery waste heat heating inlet material system components, wherein: the gas fractionation heating system components include: fractionation towers, air coolers, Water-cooled heat exchanger and reboiler, the top material outlet of the fractionation tower is connected to the material side inlet of the air cooler, the material side outlet of the air cooler is connected to the material side inlet of the water-cooled heat exchanger; the water side of the water-cooled heat exchanger is connected to the circulating cooling water system; reboil The low-temperature side of the reboiler is connected to the fractionation tower, and the high-temperature side of the reboiler is connected to the high-temperature process steam; the system components for recovering waste heat and heating imported materials include: hot water/material heat exchanger and steam-type lithium bromide absorption heat pump, wherein: hot water/ The material side of the material heat exchanger is connected to the material inlet of the fractionation tower, the hot water/material heat exchanger is connected to the steam type lithium bromide absorption heat pump condenser and absorber, the steam type lithium bromide absorption heat pump generator is connected to high temperature process steam, steam type The lithium bromide absorption heat pump evaporator is connected to circulating cooling water; the hot water/material heat exchanger is used to preheat the material outside the fractionation tower to 80±10°C. The boiler is heated and maintained at the working temperature required for material fractionation to realize cascade heating of materials.
所述热水/物料换热器的加热热源是回收分馏塔塔顶出口产品热物料余热制备的热水，或是石油炼化的其它工艺环节热联合余热热媒水。The heating heat source of the hot water/material heat exchanger is the hot water prepared by recovering the waste heat of the hot material exported from the top of the fractionation tower, or the heat combined with waste heat heat medium water in other process links of petroleum refining.
所述物料分馏所需的工作温度为110±10℃。The working temperature required for the material fractionation is 110±10°C.
所述的蒸汽型溴化锂吸收式热泵能够被石油炼化的其它工艺环节热联合余热热媒水管道所替代，其中：热水/物料换热器低温侧接分馏塔物料入口，热水/物料换热器高温侧接石油炼化的其它工艺环节热联合余热热媒水管道。The steam-type lithium bromide absorption heat pump can be replaced by heat-combined waste heat heat medium water pipelines in other process links of petroleum refining, wherein: the low-temperature side of the hot water/material heat exchanger is connected to the material inlet of the fractionation tower, and the hot water/material exchange The high temperature side of the heater is connected to the heat joint waste heat heat medium water pipeline of other process links in petroleum refining.
本发明的有益效果是：回收原本散失到环境中的分馏塔塔顶产品物料余热，或者利用石油炼化的其它工艺环节热联合余热，用于对进口物料进行预热，实现了分馏塔加热工艺的能量梯级利用，降低工艺蒸汽消耗量20％以上，提高了分馏塔工艺流程的能源利用效率，进而节约生产成本。The beneficial effects of the present invention are: recovery of the waste heat of the top product material of the fractionation tower originally lost to the environment, or use of heat combined with waste heat in other process links of petroleum refining to preheat the imported materials, and realize the heating process of the fractionation tower The cascade utilization of energy reduces the consumption of process steam by more than 20%, improves the energy utilization efficiency of the fractionation tower process, and thus saves production costs.
附图说明Description of drawings
图1是常规分馏塔工艺系统流程简图。Figure 1 is a schematic flow chart of a conventional fractionation tower process system.
图2是利用溴化锂吸收式热泵和工艺蒸汽对进口物料梯级加热的分馏塔工艺系统流程简图。Fig. 2 is a schematic flow chart of a fractionation tower process system using a lithium bromide absorption heat pump and process steam to heat imported materials in steps.
图3是利用石油炼化的其它工艺环节热联合余热热媒水和工艺蒸汽对进口物料梯级加热的分馏塔工艺系统流程简图。Fig. 3 is a schematic flow diagram of a fractionation tower process system for cascade heating of imported materials by using heat from other process links of petroleum refining combined with waste heat heat medium water and process steam.
图中：1.分馏塔，2.重沸器，3.空冷器，4.水冷换热器，5.热水/物料换热器，6.蒸汽型溴化锂吸收式热泵，7.阀门，P1.物料进口管道，P2.塔顶产品物料出口管道，P3.塔底产品物料出口管道，P4.工艺蒸汽管道，P5、P6.疏水管道，P7.循环冷却水高温管道，P8.循环冷却水低温管道，P9.热联合余热热媒水高温管道，P10.热联合余热热媒水低温管道，A.吸收器，C.冷凝器，E.蒸发器，G.发生器。In the figure: 1. Fractionation tower, 2. Reboiler, 3. Air cooler, 4. Water-cooled heat exchanger, 5. Hot water/material heat exchanger, 6. Steam type lithium bromide absorption heat pump, 7. Valve, P1 .Material inlet pipeline, P2. Tower top product material outlet pipeline, P3. Tower bottom product material outlet pipeline, P4. Process steam pipeline, P5, P6. Drainage pipeline, P7. Circulating cooling water high temperature pipeline, P8. Circulating cooling water low temperature Pipeline, P9. High-temperature pipeline of heat combined with waste heat heat medium, P10. Low temperature pipeline of heat combined with waste heat heat medium, A. Absorber, C. Condenser, E. Evaporator, G. Generator.
具体实施方式detailed description
下面结合附图和实施例对本发明进一步说明。The present invention will be further described below in conjunction with the accompanying drawings and embodiments.
实施例1：Example 1:
在图2所示的流程2中，物料进口管道P1分别与热水/物料换热器5的物料侧入口51和阀门7的进口相连，分馏塔1的物料入口11分别与阀门7的出口和热水/物料换热器5的物料侧出口52相连，分馏塔1的塔顶高温产品物料出口12与空冷器的入口相连，分馏塔1塔底成品物料接塔底产品出口管道P3，分馏塔1塔底物料出口13与重沸器2的低温侧进口21相连，分馏塔1塔底物料进口14与重沸器2的低温侧出口22相连；空冷器3的出口与水冷换热器4的物料入口41相连；水冷换热器4的物料出口42与塔顶成品出口管P2相连，水冷换热器4的循环冷却水进口43与循环冷却水低温管道P8相连，循环冷却水出口44与循环冷却水高温管道P7相连；蒸汽型溴化锂吸收式热泵6的蒸发器E接口65、66分别与循环冷却水高温管道P7、循环冷却水低温管道P8相连，吸收器A和冷凝器C接口63、64分别与热水/物料换热器的高温侧接口54、53相连，发生器G接口61、62分别与工艺蒸汽管道P4、疏水管道P6相连；重沸器的高温侧接口23、24分别与工艺蒸汽管道P4、疏水管道P5相连。In the flow process 2 shown in Figure 2, the material inlet pipeline P1 is connected with the material side inlet 51 of the hot water/material heat exchanger 5 and the inlet of the valve 7 respectively, and the material inlet 11 of the fractionating tower 1 is connected with the outlet of the valve 7 and the inlet of the valve 7 respectively. The material side outlet 52 of the hot water/material heat exchanger 5 is connected, the high-temperature product material outlet 12 at the top of the fractionation tower 1 is connected with the inlet of the air cooler, and the finished product material at the bottom of the fractionation tower 1 is connected to the bottom product outlet pipeline P3, and the fractionation tower 1 The tower bottom material outlet 13 is connected with the low-temperature side inlet 21 of the reboiler 2, and the fractionation tower 1 tower bottom material inlet 14 is connected with the low-temperature side outlet 22 of the reboiler 2; the outlet of the air cooler 3 is connected with the water-cooled heat exchanger 4 The material inlet 41 is connected; the material outlet 42 of the water-cooled heat exchanger 4 is connected with the tower top product outlet pipe P2, the circulating cooling water inlet 43 of the water-cooled heat exchanger 4 is connected with the circulating cooling water low temperature pipeline P8, and the circulating cooling water outlet 44 is connected with the circulating cooling water The cooling water high-temperature pipeline P7 is connected; the evaporator E ports 65 and 66 of the steam-type lithium bromide absorption heat pump 6 are respectively connected with the circulating cooling water high-temperature pipeline P7 and the circulating cooling water low-temperature pipeline P8, and the absorber A and condenser C interfaces 63 and 64 They are respectively connected to the high temperature side ports 54 and 53 of the hot water/material heat exchanger, and the generator G ports 61 and 62 are respectively connected to the process steam pipe P4 and the drain pipe P6; the high temperature side ports 23 and 24 of the reboiler are respectively connected to the process The steam pipeline P4 and the drain pipeline P5 are connected.
系统工作时，物料由物料进口管道P1进入热水/物料换热器进行加热，温度升至80±10℃后经物料入口11进入分馏塔1，在塔内被塔底重沸器加热并维持至110℃左右，实现物料的梯级加热。塔顶产品依次经空冷器3和水冷换热器4到达产品物料出口管道P2；塔底物料由塔底物料出口13进入重沸器2，加热后经塔底物料进口14进入分馏塔1。When the system is working, the material enters the hot water/material heat exchanger from the material inlet pipe P1 for heating. After the temperature rises to 80±10°C, it enters the fractionation tower 1 through the material inlet 11, and is heated and maintained by the reboiler at the bottom of the tower. To about 110 ℃, realize the cascade heating of materials. The top product passes through the air cooler 3 and the water-cooled heat exchanger 4 to the product material outlet pipeline P2 in turn; the tower bottom material enters the reboiler 2 from the tower bottom material outlet 13, and enters the fractionation tower 1 through the tower bottom material inlet 14 after heating.
循环冷却水系统通过水冷换热器4将塔顶产品物料的大量余热带走，升温后的循环冷却水通往蒸汽型溴化锂吸收式热泵6的蒸发器E，作为蒸汽型溴化锂吸收式热泵6的低温热源，利用少量高温工艺蒸汽作为驱动热源，制备的中温热水，该中温热水作为热水/物料换热器5的热源，由此实现回收蕴含在循环冷却水中的塔顶物料余热。The circulating cooling water system takes away a large amount of residual heat of the tower top product material through the water-cooled heat exchanger 4, and the heated circulating cooling water leads to the evaporator E of the steam-type lithium bromide absorption heat pump 6, and serves as the steam-type lithium bromide absorption heat pump 6. The low-temperature heat source uses a small amount of high-temperature process steam as the driving heat source to prepare medium-temperature hot water. The medium-temperature hot water is used as the heat source of the hot water/material heat exchanger 5, thereby realizing the recovery of the waste heat of the tower top material contained in the circulating cooling water .
实施例2：Example 2:
若石油炼化厂其它工艺(如常减压、催化裂化)生产有富余的品位低于工艺蒸汽的热联合余热热媒水，可将蒸汽型溴化锂吸收式热泵替换为热联合热媒水循环管路P9、P10，作为热水/物料换热器的热源，其他连接方式及工作原理同实施例1，其流程如图3所示。If other processes in the petroleum refinery (such as atmospheric and vacuum, catalytic cracking) produce surplus heat-combined waste heat heat medium water with a grade lower than process steam, the steam-type lithium bromide absorption heat pump can be replaced by heat-combined heat medium water circulation pipeline P9 , P10, as the heat source of the hot water/material heat exchanger, other connection methods and working principles are the same as in Embodiment 1, and its flow process is shown in Figure 3.
本发明中新增的热水/物料换热器5、蒸汽型溴化锂吸收式热泵6以及阀门7均为成熟产品。各设备的具体实施方式分别说明如下：The newly added hot water/material heat exchanger 5, steam-type lithium bromide absorption heat pump 6 and valve 7 in the present invention are all mature products. The specific implementation of each device is described as follows:
1.分馏塔，根据物料生产量确定，为常用设备；1. Fractionation tower, determined according to the material production volume, is a common equipment;
2.重沸器，根据物料生产量、进料温度和塔内物料温度确定，为常用设备；2. Reboiler, determined according to the material production volume, feed temperature and material temperature in the tower, is a common equipment;
3.空冷器，根据塔顶物料的生产量、要求的成品物料冷却温度确定，为常用设备；3. The air cooler is a commonly used equipment determined according to the production volume of the tower top material and the required cooling temperature of the finished material;
4.水冷换热器，根据塔顶物料的生产量、要求的成品物料冷却温度确定，为常用设备；4. The water-cooled heat exchanger is a commonly used equipment determined according to the production volume of the tower top material and the required cooling temperature of the finished material;
5.热水/物料换热器，根据进口物料流量和加热温度确定，为非标设计设备；5. The hot water/material heat exchanger is determined according to the imported material flow and heating temperature, and is a non-standard design equipment;
6.蒸汽溴化锂吸收式热泵，根据工艺蒸汽压力、塔顶余热量及温度和热水/物料换热器的需热量及温度确定，此为非标设计设备；6. The steam lithium bromide absorption heat pump is determined according to the process steam pressure, the residual heat and temperature at the top of the tower, and the required heat and temperature of the hot water/material heat exchanger. This is a non-standard design equipment;
7.阀门，根据管径确定大小。7. The size of the valve is determined according to the pipe diameter.
本发明的加热系统是在分馏塔物料加热工艺原有流程的基础上，于分馏塔物料进口处增设了热水/物料换热器，利用蒸汽型溴化锂吸收式热泵回收气体分馏塔塔顶余热，对进口物料预热的梯级加热流程2如图2所示；利用其它石化工艺热联合余热热媒水实现进口物料预热的梯级加热流程3如图3所示。该方法可以减少醇胺再生、脱丙烷、催化蒸馏等工艺的分馏塔加热环节的熵增，实现、能源的合理利用，节约生产消耗的工艺蒸汽。The heating system of the present invention is based on the original process of the material heating process of the fractionation tower, and a hot water/material heat exchanger is added at the material inlet of the fractionation tower, and a steam-type lithium bromide absorption heat pump is used to recover the waste heat at the top of the gas fractionation tower. The cascade heating process 2 for preheating imported materials is shown in Figure 2; the cascade heating process 3 for preheating imported materials by using other petrochemical process heat combined with waste heat heat medium water is shown in Figure 3. The method can reduce the entropy increase in the heating link of the fractionation tower in processes such as alcohol amine regeneration, depropanization, catalytic distillation, etc., realize rational utilization of energy, and save process steam consumed in production.
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